Process and apparatus to determine the degree of separation of two solution streams

ABSTRACT

The invention provides a method, and apparatus, for determining the degree of separation (DOS) of a polymer solution into a polymer-rich stream and a solvent-rich stream, said method comprising the following:
         adding to a liquid-liquid separation vessel the polymer solution, which comprises a polymer, a solvent and an anti-solvent;   separating the polymer solution into a polymer-rich stream and a solvent-rich stream;   removing at least some the polymer-rich stream from at least one outlet P on the vessel, and measuring the actual solution density of this polymer-rich stream using at least one flow meter;   removing at least some of the solvent-rich stream from at least one other outlet S on the vessel, and measuring the actual density of the solvent-rich stream using at least one flow meter; and   wherein the degree of separation (DOS) is determined by the following equation (Eqn. 1):
 
DOS=[actual solution density (polymer-rich steam)−actual solution density (solvent-rich stream)]/[theoretical solution density (polymer-rich stream)−theoretical solution density (solvent-rich stream)]  (Eqn. 1).

BACKGROUND

A liquid-liquid separator is used in solution polymerizations toseparate the solvent and unreacted monomers (in a solvent-rich stream)from the polymer (in a polymer-rich stream). The degree of separation isinfluenced by the process conditions, such as, for instance, the amountof anti-solvent (e.g., propane), the amount unreacted monomers in theinlet stream, the inlet stream temperature, and the adiabatic pressuredrop into the separator. However, the degree of separation is typicallynot realized, until undesirable polymer carry over is detected in thesolvent recovery downstream equipment. Thus, there is a need for amethod to determine the degree of separation of solvent and unreactedmonomers from the polymer, early on, in the “work-up process” of polymersolution, and which would allow for the on-line adjustment ofpolymerization conditions to improve the degree of separation.

Polymerization processes and/or polymer separation processes aredisclosed in the following references: International Publications,WO2012/156393, WO2002/034795, WO2011/008955; US2012/0277392; Zhang etal., Phase Behavior, Density, and Crystallization of Polyethylene inn-Pentane and in n-Pentane/CO2 at High Pressures, Journal of AppliedPolymer Science (2003), Vol. 89, 2201-2209; Ehrlich et al., PhaseEquilibria of Polymer-Solvent Systems at High Pressures Near TheirCritical Loci: Polyethylene with n-Alkanes, Journal of Polymer Science(1963), Part A, Vol. 1, 3217-3229; De Loos et al, Liquid-liquid PhaseSeparation in Linear Low Density Polyethylene-Solvent Systems, FluidPhase Equilibria (1996), 117(1-2), 40-7; Buchelli et al., On-LineLiquid-Liquid Phase Separation Predictor in the High-DensityPolyethylene Solution Polymerization Process, Industrial & EngineeringChemistry Research (2007), 46(12), 4307-4315.

However, the separation process of the above art does not allow for realtime feedback of the degree of separation of the polymer solution into apolymer-rich stream and a solvent-rich stream. As discussed, thereremains a need for a method to determine the degree of separation ofsolvent and unreacted monomers from the polymer, early on, in thework-up process of polymer solution, and which would allow for theon-line adjustment of polymerization conditions to improve the degree ofseparation. These needs have been met by the following invention.

SUMMARY OF INVENTION

A novel, non-intrusive technique has been developed to determine thedegree of separation of two solutions, a polymer-rich stream and asolvent-rich stream. This technique utilizes flow meters (for example,coriolis meters) to measure the actual density of each stream(solvent-rich stream and polymer-rich stream) exiting a liquid-liquidseparation vessel.

The invention provides a method for determining the degree of separation(DOS) of a polymer solution into a polymer-rich stream and asolvent-rich stream, said method comprising the following:

adding to a liquid-liquid separation vessel the polymer solution, whichcomprises a polymer, a solvent and an anti-solvent;

separating the polymer solution into a polymer-rich stream and asolvent-rich stream;

removing at least some the polymer-rich stream from at least one outletP on the vessel, and measuring the actual solution density of thispolymer-rich stream using at least one flow meter;

removing at least some of the solvent-rich stream from at least oneother outlet S on the vessel, and measuring the actual density of thesolvent-rich stream using at least one flow meter; and

wherein the degree of separation (DOS) is determined by the followingequation (Eqn. 1):DOS=[actual solution density (polymer-rich steam)−actual solutiondensity (solvent-rich stream)]/[theoretical solution density(polymer-rich stream)−theoretical solution density (solvent-richstream)]  (Eqn. 1).

The invention also provides an apparatus for determining the degree ofseparation (DOS) of a polymer solution into a polymer-rich stream and asolvent-rich stream, said apparatus comprising at least the following;

a liquid-liquid separation vessel comprising at least one outlet P andat least one outlet S;

at least two flow meters; and

wherein at least one flow meter is in contact with at least some of thepolymer-rich stream that exits the vessel via outlet P; and

wherein at least one other flow meter is in contact with at least someof the solvent-rich stream that exits the vessel via outlet S.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 depicts a solution polymerization process comprising an inventiveapparatus used to determine the degree of separation (DOS) of a polymersolution into a polymer-rich stream and a solvent-rich stream. Forexample, the solution polymerization of EPDM, where [M]=ethylene,propylene, ENB, [H]=hydrogen, [C]=catalyst, [L]=anti-solvent, and[K]=catalyst-kill.

FIG. 2 is a schematic of an inventive apparatus used to determine thedegree of separation (DOS) of a polymer solution into a polymer-richstream and a solvent-rich stream.

DETAILED DESCRIPTION

As discussed above, the invention relates a method for determining thedegree of separation (DOS) of a polymer solution into a polymer-richstream and a solvent-rich stream, said method comprising the following:

adding to a liquid-liquid separation vessel the polymer solution, whichcomprises a polymer, a solvent and an anti-solvent;

separating the polymer solution into a polymer-rich stream and asolvent-rich stream;

removing at least some the polymer-rich stream from at least one outletP on the vessel, and measuring the actual solution density of thispolymer-rich stream using at least one flow meter;

removing at least some of the solvent-rich stream from at least oneother outlet S on the vessel, and measuring the actual density of thesolvent-rich stream using at least one flow meter; and

wherein the degree of separation (DOS) is determined by the followingequation (Eqn. 1):DOS=[actual solution density (polymer-rich steam)−actual solutiondensity (solvent-rich stream)]/[theoretical solution density(polymer-rich stream)−theoretical solution density (solvent-richstream)]  (Eqn. 1).

An inventive method may comprise a combination of two or moreembodiments described herein.

In one embodiment, the theoretical solution density of the polymer-richstream and the theoretical solution density of the solvent-rich streamare each determined using computer software for modeling asymmetricfluid systems. In a further embodiment, the computer software is asoftware for thermodynamic modeling of asymmetric fluid systems, andfurther a VLXE* software (for example, VLXE 4.5). See www.vlxe.com.

In one embodiment, the outlet P is located below the outlet S.

In one embodiment, the polymer is an olefin-based polymer.

In one embodiment, the polymer is selected from an ethylene-basedpolymer or a propylene-based polymer.

In one embodiment, the DOS is from 0.80 to 1.20, further from 0.85 to1.15, further from 0.90 to 1.10, and further from 0.95 to 1.05.

In one embodiment, the polymer solution is separated into thepolymer-rich stream and the solvent-rich stream by a reduction in thepressure in the liquid-liquid separation vessel. In a furtherembodiment, the pressure is reduced at a control rate.

The invention also provides an apparatus for determining the degree ofseparation (DOS) of a polymer solution into a polymer-rich stream and asolvent-rich stream, said apparatus comprising at least the following;

a liquid-liquid separation vessel comprising at least one outlet P andat least one outlet S;

at least two flow meters; and

wherein at least one flow meter is in contact with at least some of thepolymer-rich stream that exits the vessel via outlet P; and

wherein at least one other flow meter is in contact with at least someof the solvent-rich stream that exits the vessel via outlet S.

An inventive apparatus may comprise a combination of two or moreembodiments described herein.

In one embodiment, the degree of separation (DOS) is determined by thefollowing equation (Eqn. 1):DOS=[actual solution density (polymer-rich steam)−actual solutiondensity (solvent-rich stream)]/[theoretical solution density(polymer-rich stream)−theoretical solution density (solvent-richstream)]  (Eqn. 1).

In one embodiment, the DOS is from 0.90 to 1.10, and further from 0.95to 1.05.

In one embodiment, the theoretical solution density of the polymer-richstream and the theoretical solution density of the solvent-rich streamare each determined using a computer software for modeling asymmetricfluid systems. In a further embodiment, the computer software is asoftware for thermodynamic modeling of asymmetric fluid systems, andfurther a VLXE* software (for example, VLXE 4.5). See www.vlxe.com.

In one embodiment, the outlet P is located below the outlet S.

In one embodiment, the polymer is an olefin-based polymer.

In one embodiment, the polymer is selected from an ethylene-basedpolymer or a propylene-based polymer.

In one embodiment, the polymer solution comprises a polymer, a solventand an anti-solvent.

In one embodiment, the polymer solution is separated into thepolymer-rich stream and the solvent-rich stream in the liquid-liquidseparation vessel, and further by a reduction in the pressure in theliquid-liquid separation vessel. In a further embodiment, the pressureis reduced at a control rate.

In one embodiment, the apparatus further comprises a pressure reducingmeans for reducing the pressure in the liquid-liquid separation vessel.

The following embodiments apply to both an inventive method and aninventive apparatus, as described above.

In one embodiment, the polymer solution comprises a polymer selectedfrom an ethylene-based polymer or a propylene-based polymer. In afurther embodiment, the polymer is an ethylene-based polymer. In yet afurther embodiment, the concentration of ethylene fed to the reactor isless than 30 weight percent, preferably less than 20 weight percent,based on the weight of feed to the reactor, if only one reactor is used,or based on the weight of the feed to each reactor, if more than onereactor is used. In a further embodiment, the ethylene-based polymer isan ethylene/alpha-olefin interpolymer. In a further embodiment, thealpha-olefin is a C3-C8, preferably a C4-C8 alpha-olefin. In a furtherembodiment, the interpolymer contains less than 30 weight percent of thealpha-olefin, based on the weight of the interpolymer.

In one embodiment, the ethylene-based polymer is an EPDM.

Examples of solvents include, but are not limited to, hydrocarbonscontaining six or more carbon atoms, and mixtures of such hydrocarbons.Such a hydrocarbon solvent does not comprise a hydrocarbon containingless than six carbon atoms, although residual amounts (typically lessthan 10,000 ppm, based on total weight of the hydrocarbon solvent) ofthese hydrocarbons may be present. Typically, such hydrocarbon solventshave a normal boiling point higher than 95° C. A “hydrocarbon,” as usedherein refers to an organic molecule made up of only carbon and hydrogenatoms. Examples of solvents include n-octane, n-nonane, iso-octane, andalkenes like internal isomers of octene (those with double bond notlocated on a terminal carbon atom).

In one embodiment, the solvent comprises a hydrocarbon containinggreater than, or equal to, 6 carbon atoms.

In one embodiment, the solvent is a hydrocarbon containing greater than,or equal to, 6 carbon atoms.

The solvent may comprise a combination of two or more embodimentsdescribed herein.

Examples of anti-solvents include, but are not limited to, hydrocarbonscontaining hydrocarbons containing five or less carbon atoms, andmixtures of such hydrocarbons. Such anti-solvents do not comprise ahydrocarbon containing more than five carbon atoms, although residualamounts (typically less than 10,000 ppm, based on total weight of thehydrocarbon anti-solvent) of these hydrocarbons may be present.Typically, such anti-solvents have a normal boiling point lower than 40°C. A “hydrocarbon,” as used herein refers to an organic molecule made upof only carbon and hydrogen atoms. Examples of anti-solvents includeethane, propane, isobutene, and the like.

In one embodiment, the anti-solvent comprises a hydrocarbon containingless than 6 carbon atoms.

In one embodiment, the anti-solvent is a hydrocarbon containing lessthan 6 carbon atoms.

The anti-solvent may comprise a combination of two or more embodimentsdescribed herein.

In one embodiment, the anti-solvent comprises at least one hydrocarboncontaining from 2 to 5 carbon atoms, further from 2 to 4 carbon atoms.

In one embodiment, the anti-solvent is selected from ethane, propane,isobutane, pentane or isopentane, or mixtures thereof, and furtherpropane or isobutane.

In one embodiment, the solvent comprises at least one hydrocarboncontaining from 6 to 10 carbon atoms, further from 7 to 9 carbon atoms.

In one embodiment, the solvent comprises at least one hydrocarboncontaining from 7 to 10 carbon atoms, further from 8 to 10 carbon atoms,further from 9 to 10 carbon atoms.

In one embodiment, the solvent is selected from n-hexane, n-heptane,n-octane, iso-octane, n-nonane, n-decane, or mixtures thereof, furthern-octane, iso-octane, n-nonane, n-decane, or mixtures thereof, andfurther n-octane.

In one embodiment, the solvent comprises a hydrocarbon with 6 or morecarbon atoms, further 7 or more carbon atoms, further 8 or more carbonatoms.

In one embodiment, the solvent comprises a hydrocarbon with 8 or morecarbon atoms, further 9 or more carbon atoms, more further 10 or morecarbon atoms.

In one embodiment, the anti-solvent comprises a hydrocarbon with 5 orless carbon atoms, further 4 or less carbon atoms, more further 3 orless carbon atoms.

In one embodiment, the anti-solvent comprises a hydrocarbon with 4 orless carbon atoms, and the solvent comprises a hydrocarbon with 6 ormore carbon atoms, further 7 or more carbon atoms, further 8 or morecarbon atoms, further 9 or more carbon atoms.

In one embodiment, the anti-solvent comprises, as a majority weightpercent, based on the weight of the anti-solvent, a hydrocarbon with 5or less carbon atoms, further 4 or less carbon atoms, and the solventcomprises, as a majority weight percent, based on the weight of thesolvent, a hydrocarbon with 6 or more carbon atoms, further 7 or morecarbon atoms, further 8 or more carbon atoms, further 9 or more carbonatoms.

The anti-solvent may comprise a combination of two or more embodimentsdescribed herein.

The solvent may comprise a combination of two or more embodimentsdescribed herein.

In one embodiment, the amount of anti-solvent is from 5 to 40 weightpercent, further from 10 to 35 weight percent, further from 15 to 30weight percent, based on the weight of the polymerization system.

In one embodiment, the anti-solvent is present in an amount from 5 to 50weight percent, further from 10 to 45 weight percent, and further from15 to 40 weight percent, based on the weight of the solvent and theanti-solvent.

In one embodiment, the solvent is present in an amount from 50 to 95weight percent, further from 55 to 90 weight percent, and further from60 to 85 weight percent, based on the weight of the solvent and theanti-solvent.

In one embodiment, the anti-solvent is present in an amount from 10 to40 weight percent, further from 15 to 35 weight percent, and furtherfrom 20 to 30 weight percent, based on the weight of the solvent and theanti-solvent.

In one embodiment, the solvent is present in an amount from 60 to 90weight percent, further from 65 to 85 weight percent, and further from70 to 80 weight percent, based on the weight of the solvent and theanti-solvent.

In one embodiment, the polymer concentration in the polymer rich streamis controlled by adjusting the amount of anti-solvent.

In one embodiment, there is no special unit operation (likedistillation), in the polymerization process, to separate the solventand anti-solvent.

In one embodiment, the polymer solution is formed in a polymerizationthat takes place in a reactor configuration selected from the groupconsisting of one of the following: (a) one reactor, and (b) two or morereactors configured in series. In a further embodiment, the each reactorin the reactor configuration does not contain a cooling system.

In one embodiment, each reactor in the reactor configuration is anadiabatic reactor.

In one embodiment, the pressure in each reactor is from 40 Bar (4 MPa)to 180 Bar (18 MPa), further from 60 Bar (6 MPa) to 160 Bar (16 MPa).

In one embodiment, the pressure in each reactor is from 90 Bar (9 MPa)to 180 Bar (18 MPa), further from 90 Bar (9 MPa) to 160 Bar (16 MPa).

In one embodiment, the pressure in each reactor is from 110 Bar (11 MPa)to 180 Bar (18 MPa), further from 110 Bar (11 MPa) to 160 Bar (16 MPa).

In one embodiment, each reactor operation temperature is greater than,or equal to, 130° C., further greater than, or equal to, 140° C.,further greater than, or equal to, 150° C., and further greater than, orequal to, 160° C.

In one embodiment, the each reactor operation temperature is from 140°C. to 220° C., further from 150° C. to 210° C., further from 160° C. to200° C.

In one embodiment, the polymerization is a continuous polymerization.

In one embodiment, the polymerization is a batch polymerization.

In one embodiment, the polymer concentration in the polymer solutionentering the liquid-liquid separation vessel is from 10 to 50 weightpercent, from 20 to 50 weight percent, from 30 to 50 weight percent,based on the weight of the polymer solution.

In one embodiment, no heat is added between each reactor and theliquid-liquid separation vessel.

In one embodiment, in the liquid-liquid separation vessel, the pressureis reduced to a pressure in the range from 80 Bar (8 MPa) to 10 Bar (1MPa), preferably from 70 Bar (7 MPa) to 30 Bar (3 MPa).

In one embodiment, in the liquid-liquid separation vessel, the polymersolution forms only two liquid phases.

In a preferred embodiment, no phase separation agent is added to thepolymer solution prior to, or within, the liquid-liquid separationvessel. In a further embodiment, no phase separation agent is added tothe polymer-rich stream after the liquid-liquid separation vessel. Someexamples of phase separation agents include H2, N2, CO, CO2, and CH4.

In one embodiment, the temperature in the liquid-liquid separationvessel is greater than, or equal to, 140° C., preferably greater than,or equal to, 160° C., and more preferably greater than, or equal to,170° C.

In one embodiment, the temperature in the liquid-liquid separationvessel is less than, or equal to, 220° C., further less than, or equalto, 215° C., further less than, or equal to, 210° C., further less than,or equal to, 205° C.

In one embodiment, the temperature in the liquid-liquid separationvessel is from 140° C. to 220° C., further from 160° C. to 210° C., andfurther from 165° C. to 205° C.

In one embodiment, the liquid-liquid separation vessel has a capacityfrom 10 to 50,000 gallons.

In one embodiment, the liquid-liquid separation vessel has a capacitygreater than, or equal to, 100 gallons.

In one embodiment, the liquid-liquid separation vessel has a capacitygreater than, or equal to, 1,000 gallons.

In one embodiment, the liquid-liquid separation vessel has a capacitygreater than, or equal to, 50,000 gallons.

In one embodiment, the liquid-liquid separation vessel has a capacityfrom 10 to 100 gallons.

In one embodiment, the liquid-liquid separation vessel has a capacityfrom 10 to 1,000 gallons.

In one embodiment, the liquid-liquid separation vessel has a capacityfrom 10 to 5,000 gallons.

In one embodiment, no mechanical mixing takes place in the liquid-liquidseparation vessel.

In one embodiment, no sonic transponder is used inside the liquid-liquidseparation vessel. In a further embodiment, no sonic transponder is notused downstream from the liquid-liquid separation vessel. In anotherembodiment, a sonic transponder is used downstream from theliquid-liquid separation vessel.

The liquid-liquid separation vessel may comprise a combination of two ormore embodiments as described herein.

Examples of suitable flow meters include, but are not limited to, MICROMOTION ELITE flow and density meters (for example, MICRO MOTION ELITECoriolis meters), available from Emerson Process Management; and PROLINEPROMASS flow meters (for example, PROLINE PROMASS 80F, 83F Coriolismeters), available from Endress and Hauser.

Definitions

The term “polymer,” as used herein, refers to a polymeric compoundprepared by polymerizing monomers, whether of the same or a differenttype. The generic term polymer thus embraces the term homopolymer(employed to refer to polymers prepared from only one type of monomer,with the understanding that trace amounts of impurities may beincorporated into a polymer), and the term interpolymer as definedhereinafter. Trace amounts of impurities, such as catalyst residues, maybe incorporated into or within a polymer.

The term “interpolymer,” as used herein, refers to polymers prepared bythe polymerization of at least two different types of monomers. Thegeneric term interpolymer thus includes copolymers (employed to refer topolymers prepared from two different types of monomers), and polymersprepared from more than two different types of monomers.

The term “olefin-based polymer,” as used herein, refers to a polymerthat comprises at least a majority weight percent, based on the weightof the polymer, polymerized olefin (for example, ethylene or propylene),and, optionally, one or more additional comonomers.

The term “ethylene-based polymer,” as used herein, refers to a polymerthat comprises at least a majority weight percent polymerized ethylene(based on the weight of polymer), and, optionally, one or moreadditional comonomers.

The term “propylene-based polymer,” as used herein, refers to a polymerthat comprises at least a majority weight percent polymerized propylene(based on the weight of polymer), and, optionally, one or moreadditional comonomers.

The term “polymer-rich phase,” as used herein, in relation to two ormore phases under consideration, refers to the phase containing thegreater concentration of polymer, as measured by its weight fraction,based on the total weight of the phase.

The term “solvent-rich phase,” as used herein, in relation to two ormore phases under consideration, refers to the phase containing thegreater concentration of solvent, as measured by its weight fraction,based on total weight of the phase.

The term “polymer-rich stream,” as used herein, in relation to two ormore streams under consideration, refers to the stream containing thegreater concentration of polymer, as measured by its weight fraction,based on the total weight of the stream.

The term “solvent-rich stream,” as used herein, in relation to two ormore streams under consideration, refers to the stream containing thegreater concentration of solvent, as measured by its weight fraction,based on total weight of the stream.

A phase, as used herein, refers to is a region of space (a thermodynamicsystem), throughout which all physical properties of a material areessentially uniform. Examples of physical properties include density,index of refraction, and chemical composition.

A liquid-liquid phase is a combination of two separate liquid phaseswhich are not miscible.

The term “liquid-liquid separation vessel (LLS),” as used herein, refersto a device used for the separation of two or more liquid phases. Theseparation results from the specific action, for example, a reduction inpressure, taken to induce two or more liquid phases.

The term “polymer solution,” as used herein, refers to the completedissolution of polymer in one or more solvents (typically much lower inmolecular weight than polymer) to form a homogeneous (most often inliquid state) phase. The solution comprises the polymer solvent, and mayalso comprise anti-solvent, unreacted monomers and other residuals ofthe polymerization reaction.

The term “solvent,” as used herein, refers to a substance (for example,a hydrocarbon (excluding monomer and comonomer)) that dissolves aspecies of interest, like a monomer and/or polymer, resulting in aliquid phase.

The term “anti-solvent,” as used herein, refers to a substance, which,when added to an existing polymer solution, has the effect of loweringthe Lower Critical Solution Temperature (LCST) at a given polymer weightfraction, and, in turn, reduces the compatibility between the solventand the polymer.

Lower Critical Solution Temperature (LCST), as used herein, is definedas the temperature, above which, a solution of fixed composition, at afixed pressure, separates into two liquid phases, and, below thistemperature, the solution exists as a single liquid phase.

The term “solution polymerization,” as used herein, refers to apolymerization process, in which the formed polymer is dissolved in thepolymerization medium (for example a solvent or solvent/anti-solventmixture), under the polymerization conditions (temperature andpressure).

The term “polymerization system,” as used herein, refers to a mixturecomprising monomers, solvent and catalyst, and which will undergopolymerization reaction under appropriate conditions. The polymerizationsystem corresponds to the total feed to the reactor.

The term “adiabatic reactor,” as used herein, refers to a reactor whichhas no active heat removal mechanism and no active heat additionmechanism.

The term “pressure reducing means,” as used herein, refers to a device,such as a control valve, that allows reduction in pressure of acontinuous stream of liquid or a fixed batch of liquid.

The phrase “actively reduced in a controlled manner,” as used herein,refers to an action, such as the use of a control valve, to reducepressure to a desired level, and at a desired rate.

The terms “comprising,” “including,” “having,” and their derivatives,are not intended to exclude the presence of any additional component,step or procedure, whether or not the same is specifically disclosed. Incontrast, the term, “consisting essentially of” excludes from the scopeof any succeeding recitation any other component, step or procedure,excepting those that are not essential to operability. The term“consisting of” excludes any component, step or procedure notspecifically delineated or listed.

Experimental

Representative Polymerization

A suitable process flow diagram of an example solution polymerization(e.g., EPDM) is shown in FIG. 1. In this schematic, one or two reactors[1, 2], each with no heat removal mechanism, is/are used in thepolymerization. A control valve positioned downstream of the reactor,and before the liquid-liquid separation vessel (LLS), is used forpressure reduction. The liquid-liquid separator vessel (LLS) [4] is usedfor separating a polymer-rich stream and a solvent-rich stream. A firststage devolatilizer [5] is used for removing solvent from thepolymer-rich stream by vaporization. A second stage devolatilizer [7] isused for additional solvent removal by operating near vacuum (5-30 mbar)conditions. The final polymer product, after subject to solvent removal(under vacuum), can be pelletized using a pelletization system [20].

This process configuration also comprises a vacuum system device [8],and a recycle solvent flash drum [11]. The solvent-rich stream exitingthe LLS can be filtered through a filter to remove polymer particles.

The polymerization is carried out in one or more adiabatic reactors. Thenumber of reactors depends on the polymer type and desired molecularweight distribution. The reactor pressure is typically from 40 Bar (4MPa) to 150 Bar (15 MPa). The reactor operating temperature is typicallyfrom 140° C. to 190° C. The reaction solvent is a mixture of a solventand an anti-solvent. Examples of suitable solvents include n-heptane,n-octane, n-decane, ISOPAR-E (mixture of C5-C10 alkanes), and the like.Examples of suitable anti-solvents include ethane, propane andisobutane. Typical anti-solvent concentrations are from 5 weight percentto 40 weight percent, based on the total weight of the polymerizationsystem (includes, for example, monomers, solvent, anti-solvent; thepolymerization system corresponds to the total feed to the reactor).

Once the polymerization is completed, the polymer solution istransferred to the LLS [4]. The pressure in the LLS is reduced (forexample, to 10-60 bar, depending on the initial pressure of the polymersolution entering the LLS) to induce a liquid-liquid separation, thusforming a polymer-rich phase and a solvent-rich phase. The polymer-richphase is separated from the solvent-rich phase within the liquid-liquidseparation vessel using gravity or an enhanced gravity device. Thesolvent-rich phase is separated, cooled, filtered, and recycled back tothe reactor [1 and/or 2]. The actual solution densities of both theseparated solvent-rich stream and the polymer-rich stream are measuredby a pair of Coriolis flow meters, at the respective LLS exit stream, asshown in FIG. 2.

The polymer-rich phase is separated, passed through a heat exchanger,and then fed to the first devolatilizer [5]. A catalyst-kill [K] isadded to the polymer-rich stream, before this stream enters the LLS, andfurther the first devolatilizer. The pressure in the first devolatilizeris reduced to form a polymer solution containing more than 50 weightpercent polymer.

For final solvent removal, the concentrated polymer-rich stream, exitingthe first devolatizer [5] is transferred to a second devolatizer [7].Here, the pressure is reduced to form polymer with residual amounts (ppmlevels) of solvent. The solvent coming out the second devolatizer iscondensed, combined with solvent from first devolatizer, and thecombined solvent is then purified, and then recycled back to the reactor[1 and/or 2]. The polymer is sent to a further material handling system,such as a pelletizer [20].

Degree of Separation (DOS)

As discussed above, once the polymerization is completed, the polymersolution is transferred to the LLS [4]. The actual solution densities ofboth the solvent-rich stream and the polymer-rich stream that exit theLLS are each measured by a Coriolis flow meter at the respective LLSexit stream, for example, as shown in FIG. 2.

The theoretical solution density of the solvent-rich stream and thetheoretical solution density the polymer-rich stream are each determinedusing a computer software for thermodynamic modeling of asymmetric fluidsystems, such as VLXE* software, VLXE 4.5. “VLXE 4.5” is a commerciallyavailable, thermodynamic program that uses algorithms to solve phaseequilibrium equations for highly asymmetric systems, involvingmacromolecules and small molecule solvents (see www.vlxe.com).

The phase diagram calculation capability in the VLXE software allowscalculation of phase boundaries, separating single phase, liquid-liquid,and vapor-liquid-liquid regions, for a given stream composition. TheVLXE software can be used to determine the desired temperature andpressure that defines the boundaries of an asymmetric fluid system. Thedensity results from two polymerizations are shown in Tables 1 and 2below. Both polymerization were run, as described above, except that 15weight percent propane was used in polymerization 1, and 20 weightpercent propane was used in polymerization 2. The weight percent ofpropane (anti-solvent) was based on the total weight of thepolymerization system (includes, for example, monomers, solvent,anti-solvent; the polymerization system corresponds to the total feed tothe reactor). The solvent in each polymerization was ISOPAR-E.

The Degree of Separation (DOS) was determined using the followingEquation 1:DOS=[actual solution density(polymer-rich)−actual solutiondensity(solvent-rich)]/[theoretical solutiondensity(polymer-rich)−theoretical solution density(solvent-rich)]  (Eqn.1).Each actual solution density was measured after the reading on eachrespective flow meter stabilized (about 40-60 minutes for a LLS vesselcapacity of 25-30 gallons).

As the DOS approaches 1, the better the separation of the solvent fromthe polymer. The DOS was 1.05 and 0.98 for polymerizations (each EPDM) 1and 2, respectively. These results indicate that excellent separation ofthe solvent from the polymer was achieved in the polymerizations using15 weight percent and 20 weight percent propane.

TABLE 1 Polymerization 1 using 15 wt % propane Theoretical solutionActual Solution Density^(a) Density (lb/ft³) (lb/ft³) Solvent-Rich 28.730.3 Polymer-Rich 34.4 36.3 Solution density Difference 5.7 6.0(polymer-rich − solvent rich) ^(a)Determined using the VLXE software.

TABLE 2 Polymerization using 20 wt % propane Theoretical Solution ActualSolution Density^(a) Density (lb/ft³) (lb/ft³) Solvent-Rich 26.7 27.3Polymer-Rich 35.5 35.9 Solution density Difference 8.8 8.6 (polymer-rich− solvent-rich) ^(a)Determined using the VLXE software.

Although the invention has been described in considerable detail in thepreceding examples, this detail is for the purpose of illustration, andis not to be construed as a limitation on the invention, as described inthe following claims.

The invention claimed is:
 1. An apparatus for determining the degree ofseparation (DOS) of a polymer solution into a polymer-rich stream and asolvent-rich stream, said apparatus comprising at least the following; aliquid-liquid separation vessel comprising at least one outlet P and atleast one outlet S; at least two Coriolis meters; and wherein at leastone Coriolis meter is in contact with at least some of the polymer-richstream that exits the vessel via outlet P; and wherein at least oneother Coriolis meter is in contact with at least some of thesolvent-rich stream that exits the vessel via outlet S.
 2. The apparatusof claim 1, wherein the degree of separation (DOS) is determined by thefollowing equation (Eqn. 1):DOS=[actual solution density (polymer-rich steam)−actual solutiondensity (solvent-rich stream)]/[theoretical solution density(polymer-rich stream)−theoretical solution density(solvent-richstream)]  (Eqn. 1).
 3. The apparatus of claim 1, wherein the theoreticalsolution density of the polymer-rich stream and the theoretical solutiondensity of the solvent-rich stream are each determined using computersoftware for modeling asymmetric fluid systems.
 4. The apparatus ofclaim 1, wherein the outlet P is located below the outlet S.
 5. Theapparatus of claim 1, wherein the polymer is selected from anethylene-based polymer or a propylene-based polymer.
 6. The apparatus ofclaim 1, wherein the liquid-liquid separation vessel has no sonictransponder.
 7. The apparatus of claim 1, wherein the polymer solutioncomprises a polymer, a solvent, and an anti-solvent.
 8. The apparatus ofclaim 7, wherein the anti-solvent comprises at least one hydrocarboncontaining from 2 to 5 carbon atoms.
 9. The apparatus of claim 8,wherein the anti-solvent is selected from the group consisting ofethane, propane, isobutane, pentane, isopentane, and mixtures.